Integrated heat management systems and processes for adsorbed natural gas storage facilities

ABSTRACT

Systems and methods for heat exchange during gas adsorption and desorption cycling, one method including removing heat from an adsorbent material during gas adsorption to the adsorbent material; storing the removed heat for later use during desorption of gas from the adsorbent material; heating the adsorbent material during desorption of gas from the adsorbent material using at least a portion of the removed heat; and recycling heat during the step of heating to prepare a working fluid for the step of removing heat via temperature reduction of the working fluid.

BACKGROUND Field

The present disclosure relates to natural gas storage via adsorption andheat management. In particular, the present disclosure shows efficientheat exchange units and processes for managing temperatures duringnatural gas adsorption and desorption processes.

Description of the Related Art

Natural gas is the portable and preferred fuel of choice around theworld. Natural gas burns more completely than other traditional fuels,including petroleum and coal; therefore, the combustion of natural gasis comparatively less harmful to the environment. Natural gas andsimilar products, including LNG, propane and other compressed-gas fuelsare much more efficient in engine and turbine combustion systems.

An important component of natural gas and sales gas is methane. Whenburned, methane emits carbon dioxide at about thirty percent less thanoil, and natural gas is considered environment-friendly compared toother fossil fuels. This is one reason for the relatively rapid growthin using natural gas for heating and electricity generation over thepast few decades.

The storage capacity of a pipe or vessel can be increased by filling itwith an adsorbent that has high adsorptive storage capacity for methane,and this technology is called adsorbed natural gas storage (ANG).Certain processes include introducing natural gas into the natural gasstorage facility, separating the natural gas into a heavy natural gascomponent and a light natural gas component, and retaining thecomponents in the storage facility. The process also includes releasingthe heavy and light natural gas components and mixing them into areleased natural gas product for power plants.

Compressed natural gas (CNG) systems and processes for transportingnatural gas require increased pressures. CNG requires greater pressuresup to about 250 bars, and this increases the cost of compression andwall thickness for large vessels which prevents inexpensivemanufacturing. With respect to liquid natural gas (LNG), LNG is the mostpractically used method for large scale exporting through ships. LNG,however, requires a re-gasification infrastructure, which makes itimpractical for independent power generators, domestic users, andnatural gas filling stations to receive LNG.

When producing electricity or natural gas for non-commercial users, asignificant problem arises for natural gas transportation networks:diurnal demand. People, unlike manufacturing plants or facilities, tendnot to be steady energy users throughout the day. People consume greateramounts of electricity during the day and into the early evening andmuch less at night and into the early morning. The higher rates ofconsumption form a “peak period of demand” and the lower rate ofconsumption creates a “non-peak period of demand.” This daily trendoccurs throughout the year.

During different seasons, however, the length of each period (longer orshorter periods of natural light requiring lesser or greater amounts ofartificial light, respectively) and the amplitude of the period (forexample, greater amounts demanded at higher and lower temperaturesversus more moderate temperatures) can change the amplitude of thedemand during the diurnal period. The location of the demand also has animpact upon what the diurnal demand is like. In cooler environments,overall daily electrical and natural gas demand is lower in the summermonths and higher in winter months as consumers use heating equipment.In warmer environments, the daily demand trends are opposite as consumeruse air conditioning units to stay cool.

Swinging electrical and natural gas consumption—not only in daily usebut also in seasonal differences—results in variability across thenatural gas transportation and production system. However, natural gasproduction is nearly constant. The supply-demand gap between natural gasproduction and total consumption results in a “gas demand lag.” The lag,without intervention, manifests itself as system pressure increases anddecreases (“swings”) across the natural gas transportation system.

Electrical generation facilities prefer constant, high-pressure naturalgas as a feedstock. Pressure swings in natural gas feed can damage theelectrical generation equipment, especially rotational equipment,including gas turbines, due to sudden inappropriate feed-to-fuel ratiosthat cause equipment slowdowns while under load.

Past solutions to mitigate pressure swings include in-line compressorsin the transportation systems. CNG booster compressors that operateduring peak demand periods attempt to maintain transportation systempressure. The loss of natural gas feed pressure can result in bothdowntime for electrical generators and dissatisfied public customers.

Using compression equipment increases operating expenses of thetransmission system because the compression equipment operates at CNGtransportation system pressure. The compression equipment also must beoperable to tolerate the shift in daily operating temperatures. In-linecompressors are expensive to maintain because they do not steadilyoperate: they start when system pressure is at a low threshold value andstop when system pressure is at a high threshold value.

Compressors, despite best maintenance practices, do inadvertently breakdown. Rotational equipment breakdowns sometimes are catastrophic,requiring weeks of downtime while delivering and tuning new units. Thesudden loss of natural gas feed pressure from a malfunction can resultin immediate downtime for downstream electrical generators and long-termdissatisfied public consumers.

One bottleneck preventing the widespread use of electrical power fromrenewable sources such as solar power is the intermittency of theseenergy sources. Solar radiation is at its peak during daylight hours andbecomes negligible during nighttime hours. Natural gas as a thermalsource to produce electricity can be used to compensate for reductionsin solar energy, or wind energy. Thus, the swing in the demand fornatural gas is expected with renewable energy as well.

Adsorption-based temporary natural gas storage systems have beenproposed. Certain systems store natural gas in an adsorption bed duringnon-peak hours and release the stored gas during peak periods. Thesesystems ensure sustainability of feed pressure to power generationplants alleviating cyclic operations of involved rotating equipment andwarrant continuous power production.

Physical adsorption of natural gas is associated with heat release, anddesorption requires supply of energy (heat) to fully extract trapped gasfrom adsorbent materials. Thus, some energy is consumed to ensureoptimum operation of adsorption-based gas storage technologies. Ameasure of how much energy is required to operate an adsorption basedgas storage unit is the isosteric heat of adsorption, or in other wordsthe amount of heat released per mole of gas adsorbed. For adsorbentmaterials with high storage capacity of natural gas such as activatedcarbons, the isosteric heat of adsorption is in the range of about 17-25kJ/mol. Certain prior art systems propose external accessory solarenergy to control the adsorption bed temperature, and the minimum energyrequired to operate a facility, for one adsorption-desorption cycle,will be in the range of about 34-50 kJ/mol.

For present gas adsorption systems to manage swing due to diurnaldemand, heat management systems are needed to efficiently managetemperatures of adsorbents during gas adsorption and desorption cycles.

SUMMARY

One embodiment of the present disclosure includes a method for heatexchange during gas adsorption and desorption cycling, the methodincluding removing heat from an adsorbent material during gas adsorptionto the adsorbent material; storing the removed heat for later use duringdesorption of gas from the adsorbent material; heating the adsorbentmaterial during desorption of gas from the adsorbent material using atleast a portion of the removed heat; and recycling heat during the stepof heating to prepare a working fluid for the step of removing heat viatemperature reduction of the working fluid.

One system of the present disclosure includes a system for heat exchangeduring gas adsorption and desorption cycling, the system including a gasadsorption unit, the gas adsorption unit in fluid communication with acooling loop adapted to cool adsorbent material of the gas adsorptionunit during an adsorption cycle, and in fluid communication with aheating loop adapted to heat the adsorbent material of the gasadsorption unit during a desorption cycle; a heat pump, wherein the heatpump is adapted to remove heat from the cooling loop and provide theremoved heat to the heating loop; a first insulated storage tank tostore chilled working fluid for the cooling loop; and a second insulatedstorage tank to store heated working fluid for the heating loop.

BRIEF DESCRIPTION OF THE DRAWINGS

These and other features, aspects, and advantages of the presentdisclosure will become better understood with regard to the followingdescriptions, claims, and accompanying drawings. It is to be noted,however, that the drawings illustrate only several embodiments of thedisclosure and are therefore not to be considered limiting of thedisclosure's scope as it can admit to other equally effectiveembodiments.

FIG. 1 is a process flow diagram for one embodiment of a system forthermal storage and heat exchange during adsorption and desorptioncycles, for example for natural gas adsorption and desorption onadsorbent materials.

FIG. 2 is a process flow diagram for one embodiment of a system forthermal storage and heat exchange during adsorption and desorptioncycles with additional heat exchange beyond that shown for FIG. 1, forexample for natural gas adsorption and desorption on adsorbentmaterials.

DETAILED DESCRIPTION

So that the manner in which the features and advantages of theembodiments of systems and methods for efficient heat exchange formanaging temperatures during natural gas adsorption and desorptionprocesses, as well as others, which will become apparent, may beunderstood in more detail, a more particular description of theembodiments of the present disclosure briefly summarized previously maybe had by reference to the embodiments thereof, which are illustrated inthe appended drawings, which form a part of this specification. It is tobe noted, however, that the drawings illustrate only various embodimentsof the disclosure and are therefore not to be considered limiting of thepresent disclosure's scope, as it may include other effectiveembodiments as well.

Embodiments disclosed here show efficient systems and methods forthermal integration in gas adsorption temporary storage facilities, suchas those used to accommodate the effects of diurnal peak demand on anatural gas source. Thermal energy storage (TES) systems are applied totimely transfer and exchange, using a fluid carrier, heat during anadsorption-desorption cycle. The TES systems include a heat pump and twoseparate, distinct, insulated tanks to store the energy carrier fluid athigh and low temperature conditions. In one embodiment, the coefficientof performance of a heat pump for heat exchange is approximately equalto 4. Thus, a minimum of about 25% of the transferred energy is requiredto operate the facility. For a gas storage system using an adsorbentmaterial with a heat of adsorption of 20 kJ/mol, the use of the TESsystems and methods can surprisingly and unexpectedly reduce the energyconsumption of the facility by up to 78%, which is equivalent toconsuming only 1.4 vol. % of stored natural gas volume (with a heatingvalue of 910 Btu/SCF).

Therefore, embodiments disclosed provide efficient adsorbed natural gasstorage facilities that store thermal energy produced when gas isadsorbed in one or more adsorption bed and utilize the thermal energy(simultaneously or at a later time, within the same adsorbed natural gasstorage facility or a different adsorbed natural gas storage facility)to facilitate gas release during peak demand periods. In the TES systemsand methods, one or more heat pump and at least two tanks are used tostore a temperature modifying fluid (working fluid), and used totransfer energy to and from the adsorption bed, at alternating high andlow temperature conditions. The heat pump includes a compressor, acondenser, an evaporator, and an expansion valve. In some embodiments,it uses a refrigerant fluid to transfer energy, removing heat from theadsorbent during an adsorption cycle and providing heat to the adsorbentduring a desorption cycle.

In some known heat pumps, the coefficient of performance isapproximately 4. Thus, given that the isosteric heat of adsorptionranges from about 17-25 kJ/mol in certain embodiments, the minimumenergy required to operate the adsorption storage facility (work neededto run the heat pump and to reject input energy) will be in the range ofabout 9-13 kJ/mol for the adsorption-desorption cycle. This translatesinto consuming a minimum of about 2.2-3.4 vol. % of the stored naturalgas with a heating value of 910 Btu/SCF. In some embodiments, with theuse of spilled solar energy during radiation peak periods to runequipment of the TES systems and methods, energy consumption can befurther reduced to 1.1-1.7 vol. % of stored gas. From this analysis, anadvantageous, surprising, and unexpected eightfold decrease in energyconsumption can be achieved by utilizing the proposed TES systems andmethods.

Referring now to FIG. 1, a process flow diagram is shown for oneembodiment of a system for thermal storage and heat exchange duringadsorption and desorption cycles, for example for natural gas adsorptionand desorption. In thermal energy storage and heat exchange adsorptionsystem 100, a compressed gas line 102 feeds compressed gas underpressure to a gas adsorption skid 104 comprising adsorbent material toadsorb gas. In some embodiments, the gas includes natural gas such asmethane, but in other embodiments compressed gas can include other typesof gas such as carbon dioxide, for example. Adsorbent materials caninclude activated carbons in addition to or alternative to zeolites,metal organic frameworks (MOF's), and polymers, or any other suitableadsorbent materials for adsorbing compressed gas.

In the example embodiment shown, gas adsorption skid 104 contains twoadsorption beds loaded with microporous material. One description of howgas is introduced to and removed from such a unit or multiple units isfound in U.S. Pat. No. 9,562,649, incorporated here by reference in itsentirety. Here, embodiments for thermal energy storage and heat exchangeare described. Generally, a temperature modifying fluid (working fluid)is introduced to gas adsorption skid 104 at a low temperature to absorband remove heat released during the adsorption stage via indirect heattransfer. The working fluid is then stored to be used later during thedesorption stage to supply needed energy (heat) to facilitate gasrelease from the adsorption bed. A heat pump 106, dashed line in FIG. 1,is used to exchange energy between separate working fluid andrefrigerant streams.

During an adsorption stage where a gas such as natural gas is introducedto gas adsorption skid 104 via compressed gas line 102, a working fluid,initially stored in tank 108 at low temperature conditions passes to achiller 110, such as for example an air cooled chiller, via line 112with control valve 114 to reduce its temperature to an appropriatevalue. Tank 108 and other tanks described and line 112 along with otherlines described can be thoroughly insulated to prevent heat or coolinglosses. Chiller 110, and other units described requiring power, can beoperated by either or both burning some of the stored gas or usingexcess solar energy, or other renewable sources such as wind, producedduring peak radiation periods or wind periods when the storage facilityis used for solar-based power plants or wind-based power plants.

Chilled working fluid, which can include either or both of liquid or gasrefrigerant or water, then flows to gas adsorption skid 104 via chilledfluid line 116 with control valve 118. After passing through coilsinside adsorption beds (not pictured) of gas adsorption skid 104 forindirect heat transfer, the chilled working fluid leaves gas adsorptionskid 104 via line 120 with control valve 122 to fill insulated tank 124at a temperature slightly lower than that of the adsorption beds of gasadsorption skid 104. During adsorption of gas such as natural gas, thechilled working fluid absorbs heat from gas adsorption skid 104,increasing its temperature. Tanks 108 and 124 are thermally insulated inthe embodiment shown to minimize heat leakage to and from the tanks.Chiller 110 is used in the embodiment shown to reject input energy tooperate heat pump 106 and is optionally used to compensate for heatleakage into tank 108 from the environment that tends to increase thetemperature of the working fluid.

During a desorption stage, working fluid stored in tank 124 is suppliedto gas adsorption skid 104. First, the working fluid passes via line 126to auxiliary heater 128, auxiliary heater 128 compensating for any heatlosses from tank 124. Next, the working fluid proceeds via line 130 to acondenser 132 to increase the working fluid's temperature to anappropriate selected target value (for heating adsorbent materials forgas release in gas adsorption skid 104). Then, the working fluidproceeds via line 134 to optional auxiliary tank 136, which in theembodiment shown is used to initiate the desorption stage. The auxiliaryheater 128 in some embodiments includes an electric heater, and its dutydepends at least in part on the heat loss rate in tank 124. In someembodiments, condenser 132 includes a shell and tube heat exchanger inwhich the working fluid passes through the shell side while arefrigerant at high temperature conditions passes through the tube side.The volume of auxiliary tank 136 depends in part on the volume of pipeconnections between auxiliary tank 136 and tank 108. Ultimately, heatedworking fluid at a target increased temperature passes to gas adsorptionskid 104 via line 138 with control valve 139 for release of gas, such asnatural gas, from adsorbent materials.

The use of auxiliary tank 136 is optional to ensure proper fluidtemperature entering adsorption skid 104 at the startup of thedesorption cycle. Fluid temperature at tank 124 is not suitable to passthrough the adsorption skid during the desorption process. In anotherembodiment, the auxiliary heater 128 can be used to increase thetemperature of the fluid to a target temperature that is suitable toheat up the adsorption bed at the startup of the desorption cycle andtank 136 is not required.

Inside heat pump 106, a refrigerant fluid is circulated to exchangeenergy/heat between working fluid exiting gas adsorption skid 104 inline 140 with control valve 141 during a desorption cycle and workingfluid from line 130 entering condenser 132. The heat pump includesevaporator 142, compressor 144, condenser 132, and expansion valve 146.Heat pump 106 operates to exchange heat as understood by those ofordinary skill in the art as refrigerant fluid is recirculated betweencondenser 132, expansion valve 146, evaporator 142, and compressor 144via lines 148, 150, 152, and 154. Once working fluid exiting gasadsorption skid 104 in line 140 during a desorption cycle passes throughevaporator 142, indirectly removing more heat from the working fluid tothe refrigerant, the working fluid passes to pump 158 via line 156 withcontrol valve 157, and then to tank 108 via line 160 to be used as achilled working fluid during an adsorption cycle for heat removal fromgas adsorption skid 104.

Equipment sizing to design a natural gas storage facility, for examplethat shown in FIG. 1 or FIG. 2, depends in part on the properties of thematerial used to adsorb methane, for example a microporous material inaddition to or alternative to other adsorbent materials. Activatedcarbons, zeolites, and metal-organic frameworks (MOFs) are advantageousmicroporous materials to be used to store natural gas. Activated carbonsexhibit relatively low cost, high adsorption capacity, and mechanicaland thermal stability for systems and processes described here.

Surface characterization of adsorbent materials includes measurements ofpore size distribution, bulk density, adsorption isotherms, andisosteric heat of adsorption, which all can be measured usingcommercially-available analytical equipment.

Once the properties of the microporous material, such as the adsorptioncapacity, bulk density and the isosteric heat of adsorption, aredetermined, the number, N_(bed), of required adsorption beds with agiven volume V_(bed), can be calculated via Equation 1:

$\begin{matrix}{N_{bed} = \frac{V_{storage}}{0.79\mspace{11mu}\left( {{V_{bed}{q\left( {P,T} \right)}\rho} + {n\left( {P,T,{V_{bed}\epsilon}} \right)}} \right)}} & {{Eq}.\mspace{14mu} 1}\end{matrix}$

In Eq. 1, V storage is the total volume (in SCF) of stored gas. V_(bed)is the volume of an adsorption bed available to be filled with theadsorbent, and E is the total porosity of the bed (dimensionless). q isthe adsorption isotherm of the selected material (in mol/kg), ρ is thebulk density of the adsorbent (in kg/m³) and n is the amount ofcompressed gas (in mol) in the void volume and is calculated using anappropriate equation of state. P (in bar) and T (in K) are the pressureand temperature of the adsorption bed, respectively.

In some embodiments, an adsorption (compressed gas charging) stageduration is longer than that of a gas desorption stage. Thus, tank,unit, and line size is determined based in part on the desorption stageusing the temperature difference between working fluid in lines 138 and140. The temperature of working fluid in line 138 is a set target value,while the temperature of working fluid in line 140 is calculated usingEquation 2:

$\begin{matrix}{\frac{\Delta H_{ads}V_{bed}{q\left( {P,T} \right)}\rho}{t_{D}} = {{UA}_{bed}\Delta T_{l\; n}}} & {{Eq}.\mspace{14mu} 2}\end{matrix}$

In Equation 2, t_(D) is the desorption duration (in seconds), ΔH_(ads)is the isoteric heat of adsorption (in kJ/mol), U is the overall heattransfer coefficient (in W/K/m²), and A_(bed) is the heat exchange area(in m²) in the adsorption bed. ΔT_(ln) is the log-mean temperaturedifference and is defined in Equation 3:

$\begin{matrix}{{\Delta T_{l\; n}} = \frac{T_{140} - T_{138}}{\ln\left( \frac{T_{140} - T}{T_{138} - T} \right)}} & {{Eq}.\mspace{14mu} 3}\end{matrix}$

In Equation 3, T_(i) is the temperature of a given stream i (in K), andT is the temperature of the adsorption bed (in K). Once the temperatureof working fluid in line 140 is obtained, the size of the tanks 108, 124can be estimated using Equation 4:

$\begin{matrix}{V = {N_{bed}\frac{\Delta H_{ads}V_{bed}{q\left( {P,T} \right)}\rho}{\rho_{f}C_{p_{f}}\Delta T}}} & {{Eq}.\mspace{14mu} 4}\end{matrix}$

Here, V is the volume of tank 124 (in m³), ρ_(f) and C_(pf) are theworking fluid's density and specific heat capacity, respectively. ΔT isthe temperature difference between working fluid in lines 138 and 140.The flow rate of the working fluid is given by V/t_(D) where t_(D) isthe desorption time. Similar to the temperature of working fluid in line138 during desorption stage, the temperature of working fluid in line116 can be used to control the adsorption bed temperature during theadsorption stage, and the temperature is set such that the circulationrate of the working fluid is given by V/t_(A) where t_(A) is theadsorption duration. The temperature of working fluid in line 120 iscalculated using Equation 2 by replacing t_(D) with the adsorptionduration.

In one embodiment for an optimum operation of a heat pump, for exampleas shown in FIG. 1, temperature of the evaporator 142 is set such thatthe refrigerant leaves the evaporator in line 152 at a temperature,T₁₅₂, in the vapor phase with a vapor fraction of 1. The pressure of theevaporator is equal to the saturation pressure of the refrigerant atT₁₅₂. In a similar way, temperature of condenser 132 is set such thatthe refrigerant leaves the condenser in line 148 at a temperature, T₁₄₈,in a liquid phase, that is the vapor fraction equal to zero. Thepressure of the refrigerant fluid in line 148 is equal to therefrigerant's saturation pressure at T₁₄₈. The efficiency of the systemof FIG. 1 is in part a function of the outlet refrigerant temperaturesof evaporator 142 and condenser 132. System efficiency is increased bydecreasing the difference between these temperatures. Therefore, thesize of required heat exchangers, evaporators, and condensers willincrease as a result of decreasing the temperature difference.

In one embodiment, heating duty of auxiliary heater 128 is calculated byassuming that tank 124 is an underground tank and heat dissipation fromthe tank follows the solution of heat transfer from a semi-infinite slabwhich is given by Equation 5:

$\begin{matrix}{{{Heat}\mspace{14mu}{dissipation}\mspace{14mu}{Rate}} = {V^{\frac{2}{3}}\frac{k\Delta T}{\sqrt{\alpha t}}}} & {{Eq}.\mspace{14mu} 5}\end{matrix}$

In Equation 5, V is the volume of the tank calculated using Equation 4.k and α are the thermal conductivity and diffusivity of the undergroundenvironment and are equal to

${k = {{0.52\mspace{14mu}\frac{W}{Km}\mspace{14mu}{and}\mspace{14mu}\alpha} = {10^{- 7}\mspace{14mu} m^{2}\text{/}s}}},$

respectively. ΔT is the temperature difference between the tank (124)and the underground environment. For chiller 110, additional duty tocompensate for heat ingress to tank 108 should be accounted for usingEquation 5 assuming that tank 108 is an underground tank. For both tanks108 and 124, the temperature of the stored working fluid therein,T_(tank) after a period of time, t, of storage is given by Equation 6:

$\begin{matrix}{T_{tank} = {T_{init} + {\left( {T_{g} - T_{init}} \right)\left\lbrack {1 - {\exp\left( {{- \frac{2k}{V^{\frac{1}{3}}\rho\; C_{p_{f}}\sqrt{\alpha}}}\sqrt{t}} \right)}} \right\rbrack}}} & {{Eq}.\mspace{14mu} 6}\end{matrix}$

Here, T_(init) is the initial tank temperature and T_(g) is theunderground environment's temperature, which is assumed to be equal to30° C. in the Examples described infra.

Example 1. Adsorbed Gas Storage Facility to Store 140,000 SCF (140 MSCF)of Natural Gas at 960 psig

In this example, similar to the system and process of FIG. 1, activatedcarbon with properties similar to those described in Esteves, I., et al.titled Adsorption of natural gas and biogas components on activatedcarbon, Separation and Purification Tech., 62, 281-296 (2008) is used asan adsorbent material. Water is used to control the adsorption bed'stemperature as a working fluid and R-134a is used as the refrigerantfluid. Table 1 lists design parameters used to simulate the performanceof the thermal energy storage system during the adsorption anddesorption stages. U is the heat transfer coefficient and A is theexchange surface area, and UA is the result of U multiplied by A.

TABLE 1 List of design parameters used and equipment size needed tostore 140 MSCF of natural gas at 960 psig. Design Parameter ValueAdsorption Capacity (mol/kg) 7 Heat of adsorption (kJ/mol) 20 TotalPorosity of bed 0.5 Bulk density (kg/m³) 500 Total bed available volume(m³) 35 Total bed UA value (kJ/° C. s) 12.9 Discharging time (hrs) 4Charging time (hrs) 8 Adsorption bed temperature (° C.) 35

During the adsorption stage, cold water stored in tank 108 at atemperature of 23° C. is used to maintain the temperature of gasadsorption skid 104 at 35° C. In this example chiller 110 includes anair cooled chiller, which is used to further cool down the water(working fluid) to a temperature of 15° C. The chilled working fluidleaves gas adsorption skid 104 via line 120 with gained heat, at atemperature of 34° C. and is stored in tank 124. The working fluidcirculation rate during the adsorption stage is 16.7 gallons per minute,and the temperature of working fluid in line 120 is calculated usingEquation 1.

During a desorption discharging cycle, heat supply to gas adsorptionskid 104 is needed in order to maintain the process at isothermalconditions and to more completely desorb natural gas. Fluid stored intank 124 is heated up using heat pump 106 to a temperature of 60° C.Auxiliary heater 128, such as an electric heater, is used to compensatefor heat losses from tank 124, if needed. Auxiliary tank 136 is used toinitiate the desorption process by supplying a hot fluid at 60° C. togas adsorption skid 104. Working fluid leaves gas adsorption skid 104via line 140 at 41° C. and passes through evaporator 142 to cool down to23° C. It is then stored in tank 108 to be used as a chilled workingfluid when the adsorption stage starts. With water as a working fluidthe circulation rate during the desorption stage is 33.4 gpm. Othersuitable working fluids, such as organic fluids or gases can be used inaddition to or alternative to water. Table 2 summarizes the operatingconditions of the thermal energy storage system in this example andbased on FIG. 1, and Table 3 summarizes the size and duties of certainequipment.

TABLE 2 Operation conditions of the adsorbed storage facility of FIG. 1in Example 1. Stream P (bar) T (° C.) 112 1.6 23.07 116 1.5 14.87 1201.4 33.82 126 1.4 33.6 130 1.4 33.82 134 1.3 60.0 138 1.3 60.0 140 1.241.09 156 1.1 23.06 160 1.6 23.4 152 3.48 5.0 154 19.08 80.3 148 18.9865.0 150 3.48 5.0

TABLE 3 Equipment duties and design parameters for Example 1 and FIG. 1.The duty of chiller 110 includes compensation for heat ingress.Equipment Design Parameters Value Evaporator 142 UA value (kJ/° C. s)6.30 Condenser 132 UA value (kJ/° C. s) 10.63 Auxiliary Heater 128 duty(kW) 1.98 Chiller 110 duty (kW) 39.65 Compressor 144 duty (kW) 74.39Pump 158 duty (kW) 0.14 Refrigerant flow rate in heat pump 106 (kg/s)1.57 Tank 124 volume (m³) 30.32 Tank 108 volume (m³) 30.32 AuxiliaryTank 136 volume (m³) 1 Estimated gas storage skid footprint (m²) 60Estimated TES system footprint (m²) 30

In some embodiments, heat pump 106 runs during a desorption stage whilethe chiller 110, such as an air cooled chiller, runs during theadsorption stage, and the total energy consumption of the adsorbedstorage facility is calculated to be 614.76 kWhr. Since power productionefficiency is about 50%, the energy consumption of the adsorbed storagefacility is equivalent to burning 4.61 MSCF of the stored gas, or 3.29vol. % of total gas volume stored.

FIG. 2 is a process flow diagram for one embodiment of a system forthermal storage and heat exchange during adsorption and desorptioncycles with additional heat exchange beyond that shown for FIG. 1, forexample for natural gas adsorption and desorption.

Example 2. Adsorbed Storage Facility to Store 140 MSCF of Natural Gas at960 psig with Additional Heat Exchange Integration

In this example for FIG. 2, activated carbon with properties describedin Esteves, I., et al. titled Adsorption of natural gas and biogascomponents on activated carbon, Separation and Purification Tech., 62,281-296 (2008) is used as an adsorbent material. Water is used as aworking fluid to control the temperature in the adsorption beds andR-134a is used as the refrigerant of the heat pump. A heat exchanger229, such as for example a shell and tube heat exchanger, is used tointegrate heat within the heating system used to keep the temperature ofthe gas adsorption vessel at appropriate temperature values. Thisincreases the efficiency of the thermal energy storage system, evenbeyond that shown for FIG. 1 and Example 1.

In FIG. 2, a process flow diagram is shown for one embodiment of asystem for thermal storage and heat exchange during adsorption anddesorption cycles, for example for natural gas adsorption anddesorption. In thermal energy storage and heat exchange adsorptionsystem 200, a compressed gas line 202 feeds compressed gas underpressure to a gas adsorption skid 204 comprising adsorbent material toadsorb gas. In some embodiments, the gas includes natural gas such asmethane, but in other embodiments compressed gas can include other typesof gas such as carbon dioxide, for example. Adsorbent materials caninclude activated carbons in addition to or alternative to zeolites andpolymers, or any other suitable adsorbent materials for adsorbingcompressed gas.

In the example embodiment shown, gas adsorption skid 204 containsadsorption beds loaded with microporous material (not pictured). Onedescription of how gas is introduced to and removed from such a unit ormultiple units is found in U.S. Pat. No. 9,562,649, incorporated here byreference in its entirety. A temperature modifying fluid (working fluid)is introduced to gas adsorption skid 204 at a low temperature, less thanthat of the adsorption beds during gas adsorption, to indirectly absorbheat released during the adsorption stage. The working fluid is thenstored to be used later during the desorption stage to supply neededenergy (heat) to facilitate gas release from the adsorption bed. A heatpump 206, dashed line in FIG. 2, is used to exchange energy betweenseparate working fluid and refrigerant streams.

During an adsorption stage where a gas such as natural gas is introducedto gas adsorption skid 204 via compressed gas line 202, a working fluid,initially stored in tank 208 at low temperature conditions passes to achiller 210, such as for example an air cooled chiller, via line 212with control valve 214 to reduce its temperature to an appropriate,pre-selected value, less than the temperature of gas adsorption skid 204during the adsorption cycle. Tank 208 and other tanks described and line212 along with other lines described can be thoroughly insulated toprevent heat or cooling losses. Chiller 210, and other units describedrequiring power, can be operated by either or both by burning some ofthe stored gas or using excess solar energy, or other renewable sourcessuch as wind, produced during peak radiation periods or wind periodswhen the storage facility is used for solar-based power plants orwind-based power plants.

Chilled working fluid, which can include either or both of liquid or gasrefrigerant in addition to or alternative to water and other fluids,then flows to gas adsorption skid 204 via chilled fluid line 216 withcontrol valve 218. After passing through coils inside adsorption beds(not pictured) of gas adsorption skid 204, the chilled working fluidleaves gas adsorption skid 204 via line 220 with control valve 222 tofill insulated tank 224 at a temperature slightly lower than that of theadsorption beds of gas adsorption skid 204. During adsorption of gassuch as natural gas, the chilled working fluid absorbs heat from gasadsorption skid 204, increasing its temperature. Tanks 208 and 224 arethermally insulated in the embodiment shown to minimize heat leakage toand from the tanks. Chiller 210 is used in the embodiment shown, but isoptional, to compensate for heat leakage into tank 208 from theenvironment that tends to increase the temperature of the working fluid.

During a desorption stage, working fluid stored in tank 224 is suppliedto gas adsorption skid 204. First, the working fluid passes via line 226to optional auxiliary heater 228, auxiliary heater 228 compensating forany heat losses from tank 224. Next, the working fluid proceeds via line227 to a heat exchanger 229, for example one or more shell and tube heatexchanger, to increase the working fluid's temperature from the heat ofthe working fluid in line 240. Next, the working fluid proceeds via line230 to a condenser 232 to increase the working fluid's temperature to anappropriate selected target value (for heating adsorbent materials forgas release in gas adsorption skid 204). Then, the working fluidproceeds via line 234 to optional auxiliary tank 236, which can be usedto initiate the desorption stage to ensure proper working fluidtemperature at the begging of a desorption cycle.

The auxiliary heater 228 in some embodiments includes an electricheater, and its duty depends at least in part on the heat loss rate intank 224. In some embodiments, condenser 232 includes a shell and tubeheat exchanger in which the working fluid passes through the shell sidewhile a refrigerant at high temperature conditions passes through thetube side. The volume of auxiliary tank 236 depends in part on thevolume of pipe connections between auxiliary tank 236 and tank 208.Ultimately, heated working fluid at a target increased temperaturepasses to gas adsorption skid 204 via line 238 with control valve 239for release of gas, such as natural gas, from adsorbent materials.

Inside heat pump 206, a refrigerant fluid is circulated to exchangeenergy/heat between working fluid exiting gas adsorption skid 204 andresulting in line 231 during a desorption cycle and working fluid fromline 230 entering condenser 232. The heat pump includes evaporator 242,compressor 244, condenser 232, and expansion valve 246. Heat pump 206operates to exchange heat as understood by those of ordinary skill inthe art as refrigerant fluid is recirculated between condenser 232,expansion valve 246, evaporator 242, and compressor 244 via lines 248,250, 252, and 254. Once working fluid exiting gas adsorption skid 204 inline 240 during a desorption cycle passes through heat exchanger 229 andevaporator 242 via line 231, removing more heat from the fluid, theworking fluid passes to pump 258 via line 256 with control valve 257,and then to tank 208 via line 260 to be used as a chilled working fluidduring an adsorption cycle for heat removal from gas adsorption skid204.

In one embodiment, during the adsorption stage, cold water stored intank 208 at a temperature of 22° C. is used to maintain the temperatureof gas adsorption skid 204 at 35° C. Chiller 210, such as an air cooledchiller, can be used to further cool down the water-based working fluidto a temperature of 15° C. The chilled working fluid leaves gasadsorption skid 204 in line 220 at a temperature of 34° C. and is storedin tank 224. Water circulation rate during the adsorption stage is 16.7gpm and the temperature of working fluid in line 220 is calculated usingEquation 1.

During the desorption cycle, heat supply to gas adsorption skid 204 isneeded in order to maintain the process at isothermal conditions andfully release adsorbed gas. Fluid stored in tank 224 at a temperature of34° C. is heated up using heat pump 206 to a temperature of 60° C.Auxiliary heater 228, for example including an electric heater, is usedto compensate for heat losses in tank 224. Auxiliary tank 236 is used toinitiate the desorption process by supplying a hot working fluid at 60°C. to gas adsorption skid 204. In addition to using heat pump 206, heatis exchanged between working fluid in lines 227 and 240. Hot workingfluid in line 240 exits gas adsorption skid 204 at 41° C., and it passesthrough heat exchanger 229 cooling down to 38° C. Working fluid in line231 passes through evaporator 242 to cool down to 22° C. It is thenstored in tank 208 to be used when the adsorption stage begins. Watercirculation rate during the desorption stage is 33.4 gpm.

Table 4 lists design parameter values used to simulate the performanceof the thermal energy storage system during the adsorption anddesorption stages in FIG. 2. Table 5 summarizes the operating conditionsof the thermal energy storage system of FIG. 2 in one embodiment, andTable 6 summarizes the sizes and duties of certain equipment.

TABLE 4 List of design parameters used to size needed equipment to store140 MSCF of natural gas at 960 psig. Design Parameter Value AdsorptionCapacity (mol/kg) 7 Heat of adsorption (kJ/mol) 20 Total Porosity of bed0.5 Bulk density (kg/m³) 500 Total beds available volume (m³) 35 Totalbeds heat exchange area (m²) 129 Discharging time (hrs) 4 Charging time(hrs) 8 Adsorption bed temperature (° C.) 35

TABLE 5 Operation Conditions of the adsorbed storage facility. StreamP(bar) T(° C.) 212 1.8 21.93 216 1.7 14.87 220 1.6 33.82 226 1.6 33.6227 1.6 33.82 234 1.4 60.0 238 1.4 60.0 240 1.3 41.09 256 1.1 21.92 2601.8 21.93 252 3.48 5.0 254 19.08 80.3 248 18.98 65.0 250 3.48 5.0 2311.2 37.42 230 1.5 37.5

TABLE 6 Equipment duties and design parameters for FIG. 2 and Example 2.The duty of chiller 210 includes compensation for heat ingress.Equipment Design Parameters Value Evaporator 242 UA value (kJ/° C. s)5.92 Condenser 232 UA value (kJ/° C. s) 9.73 Heat Exchanger 229 UA value(kJ/° C. s) 11.75 Auxiliary Heater 228 duty (kW) 1.98 Chiller 210 duty(kW) 35.12 Compressor 244 duties (kW) 63.94 Pump 258 duty (kW) 0.14 HeatPump 206 Refrigerant flow rate (kg/s) 1.35 Tank 224 volume (m³) 30.32Tank 208 volume (m³) 30.32 Tank 236 volume (m³) 1 Estimated gas storageskid footprint (m²) 60 Estimated TES system footprint (m²) 30

In some embodiments, heat pump 206 runs during the desorption stagewhile chiller 210 runs during the adsorption stage, and the total energyconsumption (for one adsorption stage and one desorption stage) of theadsorbed storage facility is calculated to be 536.74 kWhr. Since powerproduction efficiency is about 50%, the energy consumption of theadsorbed storage facility is equivalent to burning 4.02 MSCF of thestored gas, or 2.88 vol. % of total amount of stored natural gas.

Example 3. Integrating the Adsorbed Storage Facility with a Solar-BasedPower Plant

In a renewable-based power plant (such as solar, wind, or any otherintermittent renewable energy source or combination thereof) that is notequipped with energy storage technology, fossil fuel can be used tocompensate for shortages in renewable power supply, for example whensolar radiation is low and the power demand is high. Since energystorage technologies are not widely used with renewable powerproduction, produced electric energy is “spilled” during low demandperiods. In this example, a method of integrating the adsorption storagefacility, described in FIG. 2 and Example 2, with such solar-based powerplants is described.

During non-peak hours when produced electricity is spilled, the gasadsorption storage facility operates on either adsorption or stand bymodes. Thus, spilled energy can be used to operate chiller 210 shown inFIG. 2. This leads to a reduction in power consumption of the adsorptionfacility in terms of burning a certain amount of stored gas or otherfossil fuels. Using the same operating conditions shown in Table 5, 1.37vol. % of total gas volume stored is needed to operate the adsorptionfacility when it is integrated with a renewable-based power plant thatdoes not store excess electric power.

This example is independent of the size of the renewable power plant.One important parameter is that the spilled energy (difference betweensupply and demand) is larger than the energy required to run thechiller.

Therefore disclosed here are methods for heat exchange during gasadsorption and desorption cycling, one method including removing heatfrom an adsorbent material during gas adsorption to the adsorbentmaterial; storing the removed heat for later use during desorption ofgas from the adsorbent material; heating the adsorbent material duringdesorption of gas from the adsorbent material using at least a portionof the removed heat; and recycling heat during the step of heating toprepare a working fluid for the step of removing heat via temperaturereduction of the working fluid.

In some embodiments, the method includes the step of storing the workingfluid during the step of recycling in an insulated tank for later use inthe step of removing heat. Still in other embodiments the methodincludes the step of chilling the working fluid prior to the step ofremoving heat. In other embodiments, at least a portion of the removedheat and at least a portion of the recycled heat are applied to increasethe temperature of the working fluid prior to the heating step. Stillother embodiments include the step of applying auxiliary heat to theworking fluid to increase the temperature of the working fluid prior tothe step of heating, beyond a temperature increase achieved by theremoved heat and the recycled heat. In yet other embodiments, the stepof storing includes the use of an insulated tank and a portion of theworking fluid. Still in other embodiments, the step of recyclingincludes the use of a heat pump, the heat pump comprising an evaporator,a compressor, a condenser, and an expansion valve, and wherein theevaporator, the compressor, the condenser, and the expansion valve arefluidly coupled for a refrigerant fluid to travel therebetween.

In certain embodiments the step of removing heat maintains thetemperature of the adsorbent material between about 25° C. and about 45°C. and the step of heating maintains the temperature of the adsorbentmaterial between about 45° C. and about 55° C. Still in otherembodiments the working fluid comprises water. In some embodiments, theadsorbent material is selected from the group consisting of: activatedcarbon, zeolites, membranes, metal organic frameworks, and combinationsof the same. In other embodiments, the adsorbent material adsorbsnatural gas. Still in other embodiments, the method includes the step ofapplying a heat exchanger prior to the step of recycling to extract heatto combine with the removed heat. In certain embodiments, the heatexchanger comprises a shell and tube heat exchanger.

In yet other embodiments of the method, the step of chilling the workingfluid comprises the use of an air cooled chiller. In still otherembodiments, the method includes the use of renewable energy to power atleast a portion of the method, the renewable energy selected from thegroup consisting of: solar power, wind power, and combinations thereof.In certain other embodiments, the renewable energy includes solar power,and the solar power is spilled solar power. Still in other embodiments,the method is powered by a portion of natural gas adsorbed to theadsorbent material, the portion of natural gas less than 5 vol. % of thetotal amount of adsorbed natural gas. In some embodiments, the method ispowered by a portion of natural gas adsorbed to the adsorbent material,the portion of natural gas less than 3 vol. % of the total amount ofadsorbed natural gas.

Additionally disclosed are systems for heat exchange during gasadsorption and desorption cycling, one system including a gas adsorptionunit, the gas adsorption unit in fluid communication with a cooling loopadapted to cool adsorbent material of the gas adsorption unit during anadsorption cycle, and in fluid communication with a heating loop adaptedto heat the adsorbent material of the gas adsorption unit during adesorption cycle; a heat pump, wherein the heat pump is adapted toremove heat from the cooling loop and provide the removed heat to theheating loop; a first insulated storage tank to store chilled workingfluid for the cooling loop; and a second insulated storage tank to storeheated working fluid for the heating loop.

In some embodiments, the system includes a chiller fluidly coupled tothe first insulated storage tank adapted to lower the temperature ofstored chilled working fluid prior to use in the cooling loop. In otherembodiments, the chiller comprises an air cooled chiller. Still in otherembodiments, the system further includes an auxiliary heater coupled tothe second insulated storage tank to increase the temperature of storedheated working fluid prior to use in the heating loop.

In certain embodiments, the heat pump comprises an evaporator, acompressor, a condenser, and an expansion valve, and wherein theevaporator, the compressor, the condenser, and the expansion valve arefluidly coupled for a refrigerant fluid to travel therebetween. Still inother embodiments, the cooling loop maintains the temperature of theadsorbent material between about 25° C. and about 45° C. and where theheating loop maintains the temperature of the adsorbent material betweenabout 45° C. and about 55° C. In yet other embodiments, the workingfluid comprises water. In certain embodiments of the system, theadsorbent material is selected from the group consisting of: activatedcarbon, zeolites, membranes, metal organic frameworks, and combinationsof the same. In certain embodiments, the adsorbent material is adaptedto adsorb natural gas. Still in other embodiments, the system includes aheat exchanger fluidly coupled to the second insulated storage tank andthe heat pump, the heat exchanger adapted to remove heat from heatedworking fluid exiting the gas adsorption unit and recycle heat to theheating loop.

In some embodiments, the heat exchanger comprises a shell and tube heatexchanger. In other embodiments, the system further includes renewableenergy to power at least a portion of the system, the renewable energyselected from the group consisting of: solar power, wind power, andcombinations thereof. Still in other embodiments, the renewable energyincludes solar power, and the solar power is spilled solar power. Insome embodiments of the system, the system is powered by a portion ofnatural gas adsorbed to the adsorbent material, the portion of naturalgas less than 5 vol. % of the total amount of adsorbed natural gas. Andin yet other embodiments, the system is powered by a portion of naturalgas adsorbed to the adsorbent material, the portion of natural gas lessthan 3 vol. % of the total amount of adsorbed natural gas. In certainembodiments, the system includes a third insulated storage tank to storeheated working fluid for the heating loop, the third insulated storagetank fluidly located between the heat pump and the gas adsorption unit,wherein the third insulated storage tank is adapted to store workingfluid heated by the heat pump.

The term “about” when used with respect to a value or range refers tovalues including plus and minus 5% of the given value or range.

The singular forms “a,” “an,” and “the” include plural referents, unlessthe context clearly dictates otherwise.

In the drawings and specification, there have been disclosed embodimentsof systems and methods for efficient heat exchange for managingtemperatures during natural gas adsorption and desorption processes, aswell as others, and although specific terms are employed, the terms areused in a descriptive sense only and not for purposes of limitation. Theembodiments of the present disclosure have been described inconsiderable detail with specific reference to these illustratedembodiments. It will be apparent, however, that various modificationsand changes can be made within the spirit and scope of the disclosure asdescribed in the foregoing specification, and such modifications andchanges are to be considered equivalents and part of this disclosure.

That claimed is:
 1. A method for heat exchange during gas adsorption anddesorption cycling, the method comprising the steps of: removing heatfrom an adsorbent material during gas adsorption to the adsorbentmaterial; storing the removed heat for later use during desorption ofgas from the adsorbent material; heating the adsorbent material duringdesorption of gas from the adsorbent material using at least a portionof the removed heat; and recycling heat during the step of heating toprepare a working fluid for the step of removing heat via temperaturereduction of the working fluid.
 2. The method according to claim 1,further comprising the step of storing the working fluid during the stepof recycling in an insulated tank for later use in the step of removingheat.
 3. The method according to claim 2, further comprising the step ofchilling the working fluid prior to the step of removing heat.
 4. Themethod according to claim 1, wherein at least a portion of the removedheat and at least a portion of the recycled heat are applied to increasethe temperature of the working fluid prior to the heating step.
 5. Themethod according to claim 4, further comprising the step of applyingauxiliary heat to the working fluid to increase the temperature of theworking fluid prior to the step of heating, beyond a temperatureincrease achieved by the removed heat and the recycled heat.
 6. Themethod according to claim 1, wherein the step of storing includes theuse of an insulated tank and a portion of the working fluid.
 7. Themethod according to claim 1, wherein the step of recycling includes theuse of a heat pump, the heat pump comprising an evaporator, acompressor, a condenser, and an expansion valve, and wherein theevaporator, the compressor, the condenser, and the expansion valve arefluidly coupled for a refrigerant fluid to travel therebetween.
 8. Themethod according to claim 1, where the step of removing heat maintainsthe temperature of the adsorbent material between about 25° C. and about45° C. and where the step of heating maintains the temperature of theadsorbent material between about 45° C. and about 55° C.
 9. The methodaccording to claim 1, wherein the working fluid comprises water.
 10. Themethod according to claim 1, wherein the adsorbent material is selectedfrom the group consisting of: activated carbon, zeolites, membranes,metal organic frameworks, and combinations of the same.
 11. The methodaccording to claim 1 wherein the adsorbent material adsorbs natural gas.12. The method according to claim 1, further comprising the step ofapplying a heat exchanger prior to the step of recycling to extract heatto combine with the removed heat.
 13. The method according to claim 12,wherein the heat exchanger comprises a shell and tube heat exchanger.14. The method according to claim 3, wherein the step of chilling theworking fluid comprises the use of an air cooled chiller.
 15. The methodaccording to claim 1, further comprising the use of renewable energy topower at least a portion of the method, the renewable energy selectedfrom the group consisting of: solar power, wind power, and combinationsthereof.
 16. The method according to claim 15, where the renewableenergy includes solar power, and the solar power is spilled solar power.17. The method according to claim 1, where the method is powered by aportion of natural gas adsorbed to the adsorbent material, the portionof natural gas less than 5 vol. % of the total amount of adsorbednatural gas.
 18. The method according to claim 1, where the method ispowered by a portion of natural gas adsorbed to the adsorbent material,the portion of natural gas less than 3 vol. % of the total amount ofadsorbed natural gas.
 19. A system for heat exchange during gasadsorption and desorption cycling, the system comprising: a gasadsorption unit, the gas adsorption unit in fluid communication with acooling loop adapted to cool adsorbent material of the gas adsorptionunit during an adsorption cycle, and in fluid communication with aheating loop adapted to heat the adsorbent material of the gasadsorption unit during a desorption cycle; a heat pump, wherein the heatpump is adapted to remove heat from the cooling loop and provide theremoved heat to the heating loop; a first insulated storage tank tostore chilled working fluid for the cooling loop; and a second insulatedstorage tank to store heated working fluid for the heating loop.
 20. Thesystem of claim 19, the system further comprising a chiller fluidlycoupled to the first insulated storage tank adapted to lower thetemperature of stored chilled working fluid prior to use in the coolingloop.
 21. The system of claim 20, wherein the chiller comprises an aircooled chiller.
 22. The system of claim 19, the system furthercomprising an auxiliary heater coupled to the second insulated storagetank to increase the temperature of stored heated working fluid prior touse in the heating loop.
 23. The system according to claim 19, whereinthe heat pump comprises an evaporator, a compressor, a condenser, and anexpansion valve, and wherein the evaporator, the compressor, thecondenser, and the expansion valve are fluidly coupled for a refrigerantfluid to travel therebetween.
 24. The system according to claim 19,wherein the cooling loop maintains the temperature of the adsorbentmaterial between about 25° C. and about 45° C. and where the heatingloop maintains the temperature of the adsorbent material between about45° C. and about 55° C.
 25. The system according to claim 19, whereinthe working fluid comprises water.
 26. The system according to claim 19,wherein the adsorbent material is selected from the group consisting of:activated carbon, zeolites, membranes, metal organic frameworks, andcombinations of the same.
 27. The system according to claim 19, whereinthe adsorbent material is adapted to adsorb natural gas.
 28. The systemaccording to claim 19, further comprising a heat exchanger fluidlycoupled to the second insulated storage tank and the heat pump, the heatexchanger adapted to remove heat from heated working fluid exiting thegas adsorption unit and recycle heat to the heating loop.
 29. The systemaccording to claim 28, wherein the heat exchanger comprises a shell andtube heat exchanger.
 30. The system according to claim 19, the systemfurther comprising renewable energy to power at least a portion of thesystem, the renewable energy selected from the group consisting of:solar power, wind power, and combinations thereof.
 31. The systemaccording to claim 30, wherein the renewable energy includes solarpower, and the solar power is spilled solar power.
 32. The systemaccording to claim 19, where the system is powered by a portion ofnatural gas adsorbed to the adsorbent material, the portion of naturalgas less than 5 vol. % of the total amount of adsorbed natural gas. 33.The system according to claim 19, where the system is powered by aportion of natural gas adsorbed to the adsorbent material, the portionof natural gas less than 3 vol. % of the total amount of adsorbednatural gas.
 34. The system according to claim 19, further comprising athird insulated storage tank to store heated working fluid for theheating loop, the third insulated storage tank fluidly located betweenthe heat pump and the gas adsorption unit, wherein the third insulatedstorage tank is adapted to store working fluid heated by the heat pump.